539603 五、發明説明（1 ) 技術背景 D£ 3 8 42 7 90 C2言己述一種透明有衝擊韌性之模塑料， 由10至90重量％之固化相A)，其爲由80- 1 00重量％(以 A爲基礎）之甲基丙烯酸甲酯和20-0重量％之一種低分子 量丙烯酸烷酯組成；和90和1 0重量％之B)，其爲分佈於 固化相中而有低於-1 玻璃溫度之堅韌相，堅韌相之平 均粒度小於130奈米，而且堅韌相粒度之不均勻性小於 0.5，是由至少50重量％(以B爲基礎）之低分子量丙丨希酸 烷酯和0.5至5重量％之接枝交聯劑或經交聯之單體，其 爲具有三或多個乙烯不飽和、自由基可聚合之基，以及視 需要另有乙烯不飽和、自由基可（共）聚合之脂肪族共單體 所組成；以及少於0.05重量％之水溶性組份C)所構成， 其間至少有1 5重量％之固化相與堅韌相作共價結合。乳態 聚合物之加工而成模塑料是在擠押機（擠壓機）內完成，尤 其是一種雙螺桿之排氣擠押機，其間之水相被以液態排除 。報告中廢水不含聚合物成分。 EP-A 0 683 028記述一種由熱塑性塑膠熔體和水相之雙 相流體混合物在一種逆向雙向螺桿擠押機內脫水之方法。 其間塑膠膠乳之膠凝’直接在擒押機之膠凝區於剪力作用 下完成於塑膠熱塑性範圍之溫度。熔體被推送局部塡滿螺 桿導程’且螺桿導程中至少有一處構成窄限而陡峭之壓力 梯度’使裝載具有內聚力之固化熔體。以此方式在固化熔 體境界之前’在重力作用下流動，使具有內聚力之水相不 與固化熔體保持接觸。使用此方法可以使具有5 5重量。/。原 539603 五、發明説明（2 ) 始水組份之乳性聚合物之水含量減至僅仍有8重量％。在 排氣擠押機中，所餘揮發性成分可在排氣區向前或向後進 一步連續排除。最後在粒化噴嘴取得之顆粒，其殘餘濕氣 僅有0.06重量％。對於三相之乳性聚合物，在被壓除之廢 水中作爲有機物質之殘餘聚合物含量爲在0.4重量％範圍 內。 DE 1 97 1 8 597 C1記述一種由熱塑性塑膠相和水相構成 之二相流體混合物之一種脫水方法，其爲利用二相流體混 合物在擠押機內膠凝，在具有對流螺桿而有脫水區之雙螺 桿擠押機中使膠凝物脫水，並藉由排氣除去濕氣成分，其 間以一單螺桿擠押機或一雙螺桿擠押機作爲第一擠押機， 其中雙螺桿擠押機爲備有同步螺桿。對於三相流體聚合物 ，將在壓除廢水中得到0.3 5重量％範圍之殘餘聚合物含量。 問題與解決方法 對於熱塑性塑膠熔體與水相成二相流體混合物之脫水， 其爲利用塑膠熔體之膠凝和從固化熔體壓除水份，在擠押 機裝置中存有問題，廢水中常含非所期望之高量聚合物， 此項問題尤其見於有微小粒度之乳性聚合物，其在通常爲 難以膠凝者；此問題也存在於具較大粒徑之乳性聚合物， 其雖可膠凝而在標準狀況中僅有少量聚合物成分存在於廢 水中，但須提高通過速率。如此通常將損及膠凝效率，因 此在廢水中之聚合物含量又再昇高。因爲所分離之水相因 而含有聚合物而受污染，不能再被利用，尤爲缺失。在廢 中聚合物含量昇高沉澱池在廢水處理時之負荷（CSB値）。 -4- 539603 五、發明説明（3 ) 結果聚合物之損耗使熱塑性塑膠熔體之產率減低。因此必 須尋求一種方法，使廢水內之聚合物含量減少。 此問題藉由一種減少廢水中聚合物含量之方法而予解決 ，使熱塑性塑膠熔體和水相所成二相流體混合物，在一擠 押機裝置中因塑膠熔體之膠凝和從固化熔體將水壓除而獲 解決，其特徵在於二相流體混合物加入於擠押機裝置之後 間接導入至少爲280t溫度之過熱水蒸汽。 發明之實施 本發明方法適合用於從熱塑性塑膠熔體和水相所成之二 相流體混合物，在脫水所得之廢水中減少聚合物含量，是 利用在擠押機裝置內使塑膠熔體膠凝並從固化熔體將水壓 除。 此方法特別適合具有50至130奈米平均粒度（重量平均 値）之乳性聚合物，其如在DE 3 8 42 796 C2之槪述及具體 之實施例所記載。粒度之不一致性可以在例如〇.2以下。 此中關鍵在於乳性聚合物是由可以用作雙層之衝擊韌性改 質劑而具有熱塑性固化相和經過交聯之堅韌相所成之膠乳 粒子所構成。 此方法進一步適合用於既有良好可膠凝之乳性聚合物’ 其爲具有超過130奈米至5 00奈米之平均粒度者’尤其自 250至400奈米，如果裝置以提高之處理量而操作’基於 此原因，廢水中聚合物含量又再如非所期望而增加。此中 尤其是被稱爲用作以三層所構成之衝擊韌性改質劑而用於 聚甲基丙烯酸甲酯之乳性聚合物，其如在EP-A 0 683 028 539603 五、發明説明（4 ) DE 1 97 1 8 597 C1中槪述與具體之實施例所記載。若以在 EP-A 0 683 028和DE 1 97 1 8 597 C1中所載之方法，提高 聚合物之通過速率，例如加倍，則有礙加熱之規則而損及 膠凝效率。因此，在廢水中原本極低之聚合物含量昇高至 逾1重量％，甚或超過2重量％。若與本發明結合，該値 在高的通過速率中已再降低1重量％以下，尤其低於0.5 重量％。 本發明因此特別適合用於膠乳，其於通常可以含有30 至50重量％之分散塑膠粒子，其平均粒度例如爲1〇〇至 500奈米。相對之水相合計爲70至50重量％，包括全部 已溶之乳化劑，可能存在之膠凝劑或其他助劑與雜質。 膠乳粒子是由熱塑性塑膠構成，爲可在擠押機加工成爲 熔融狀態。此外熱塑性塑膠屬於具有50至3 00°C之玻璃轉 變溫度或在足耐分解之熔融狀態之溫度範圍內。在雙螺桿 擠押機內之熔融溫度通常在100與25 0°C之間。 熱塑性塑膠之重要種類爲以丁二烯、苯乙烯和視需要面 用之丙烯腈等爲基礎之共聚物，以及聚氯乙烯、聚丙烯酸 酯或聚甲基丙烯酸酯。更爲重要之種類爲多相熱塑性塑膠 之各種膠乳，所含膠乳粒子具有熱塑性固化相和經交聯之 堅韌相。在此方法當中，如有需要，可以用其他以固態或 熔融狀加入於雙螺桿擠押機之熱塑性塑，其且爲與膠乳之 固化相塑膠一致或與之相容者，予以混合。 固化相塑膠較佳爲由聚甲基丙烯酸甲酯組成，而堅韌相 塑膠多由交聯之聚丙烯酸丁酯組成，其若爲謀調整折射率 -6- 539603 五、發明説明（5 ) 以配合聚甲基丙烯酸甲酯，可與苯乙烯或丙烯酸苯甲酯作 爲混合聚合。此類之典型混合，例如含有4至5 0重量％之 多相膠乳-塑膠，其爲可由聚丙烯酸丁酯組分2至80重量 %和聚甲基丙烯酸甲酯組分20至98重量％組成所構成； 以及2至60重量％之熱塑性聚甲基丙烯酸甲酯塑膠。如果 被加入者不是在熔融狀態，則也可能是與聚甲基丙烯酸甲 酯膠液混合之多相塑塑膠乳，而且依本發明方法將膠乳聚 合物加工。 用於使乳性聚合物脫水之擠押機裝置一般含有一個膠凝 區’膠乳在其中膠凝，在其間以高於水蒸汽壓力之運轉壓 力，其爲利用剪力元件，如捏混-，混合-或擠塞等區段， 使相之分離開始。另有一脫水區段存在，從中將水液除去 。此時水溶性組分如乳化劑或電解質者亦被分離除去。 一排氣區段以加壓壓實之擠塞區段與脫水區段隔離。並 且用於進一步脫水。最後是一泵區段用於重新建立壓力並處 理ί谷體之卸出。此等功能可以分佈於多個機組或擠押機上。 擠押裝置可以由一具有逆向螺桿之雙螺桿擠押機構成， 在其中進行塑膠熔體之膠凝和從固化熔體將水壓除。如此 之裝置和對應之方法例如載於ΕΡ-Α 0 683 028之中。 擠押裝置尙可由一單螺桿擠押機或一具有同向螺桿所構 成之雙螺桿擠押機，在其中進行膠凝；接著由一具有逆向 螺桿所構成之雙螺桿擠押機進行膠凝和壓除等作用。如此 之裝置和對應之方法載於DE 197 18 597 C1。 依據本發明方法之進行，在由熱塑性塑膠熔體和水相所 539603 五、發明説明（6 ) 成二相流體混合物加入於擠押機置之後’直接導入過熱水 蒸汽，至少具有280°C之溫度，較佳爲290至3 00°C，以 3 00至3 20°C爲特佳。導入於擠押機時之對應壓力爲25至 35巴，特別是在28至32巴。被導入之水蒸汽量例如可爲 每小時1至1 〇公斤水，較佳爲2至8公斤，以4至6公 斤，相對於10至20公斤待脫水塑膠/水混合物之處理量。 加料是用適當之機具完成，例如一具有物料流量計之給 水泵和一電熱而爲分離之蒸汽產生器。實驗室裝置例如可 以用一熱功率自1 〇至1 5仟瓦之蒸汽產生器而設置。其間 在蒸汽產生器出口例如310°C熱水蒸汽，其蒸汽壓約在50 巴之範圍，而在擠押機入口處約在30巴之範圍。 從雙螺桿擠押機卸出已脫水之塑膠爲熔體形狀。此可藉 助於成粒噴出之存在，從中擠出許多薄條，冷卻至軟化溫 度以下，切成商業通用之模塑顆粒，然而也可直接用適當 的擠押模嘴以已知方式擠出形成塑膠型材，例如一種薄膜。 實施例 實施例U比較例） 加工後一種以二階段構成之乳性聚合物（用於PMMA模 塑料之衝擊韌性改質劑），具有如下之組成：（括符內爲用 縮簡符號表示單體組成之質量比） 階段I :丙烯酸丁酯/甲基丙烯酸醯丙酯之比例爲98:2 階段Π :甲基丙烯酸甲酯/丙烯酸丁酯/3-(2-苯並三唑基）-2-羥-5-第三辛基苯甲基甲基丙烯酸醯胺之比例： (89.1 ： 8.0 ： 2.9) 539603 五、發明説明（7 ) I / Π 質量比=33.4/66.6 聚合物相/水相之質量比=40/60 平均粒度：約60奈米 用一流量爲1 5公斤/小時之薄膜計量泵將膠乳泵入一密 封之逆向雙螺桿擠押機之機缸（區段1)內。螺桿直徑爲34 毫米。螺桿爲螺距30毫米之三螺線。螺桿轉數爲1 1 5轉/ 分。 膠凝區段長度爲600毫米並自區段1起分成五區段（區 段1至5)。 在擠押機內各膠凝區段之規定溫度爲：區段1 : 260°C/ 區段 2 : 270°C /區段 3 : 25 0°C /區段 4 : 24 0°C /區段 5 : 170〇C。 在區段5隨接一脫水區段，裝備止回螺桿，長度爲1 20 毫米。 在脫水區段中，兩缸體之最低處開有寬2毫米而長60 毫米之開隙。在此兩開口之下壓緊裝置收集槽。 用於析出之水之收集槽，經由管路保持在40巴之氮氣 壓力。用閥控制液面使排出5.27公斤/小時之水量。經由 一閥調節對後接排氣擠押機之注入，使在閥前保持熔體壓 力恆爲80巴。在排氣擠押機中之注入物保持8重量％之水 〇 在排氣擠押機（螺桿直徑30毫米）內經由兩個排氣區段 排除殘存物之揮發部份。第一排氣壓之壓力爲1 00毫巴， 隨後之排氣壓爲1 0毫巴。在粒化模咀所得擠出物或顆粒 -9 - 539603 五、發明説明（8 ) 具有0.06重量％之殘餘濕氣。 在脫水區段所析出之水具有2重量％之聚合物含量。 宣施例2(根據本發明） 如在實施例1中之方法，不同之處爲在第二階段之成乳 性聚合物加入於擠押裝置之後直接以過熱水蒸汽加入。539603 V. Description of the invention (1) Technical background D £ 3 8 42 7 90 C2 has described a transparent and impact tough molding compound from 10 to 90% by weight of the solidified phase A), which is from 80 to 100% by weight % (Based on A) of methyl methacrylate and 20-0% by weight of a low molecular weight alkyl acrylate; and 90 and 10% by weight of B), which are distributed in the cured phase with less than -1 Tough phase at glass temperature, the average particle size of the tough phase is less than 130 nm, and the non-uniformity of the tough phase particle size is less than 0.5. And 0.5 to 5% by weight of a graft-crosslinking agent or a cross-linked monomer, which has three or more ethylenically unsaturated, radically polymerizable groups, and optionally, ethylenically unsaturated, radically polymerizable (Co) polymerized aliphatic co-monomer composition; and less than 0.05% by weight of water-soluble component C), with at least 15% by weight of the solidified phase and the tough phase covalently bonded. The processing of milky polymers into molding compounds is done in an extruder (extruder), especially a twin-screw exhaust extruder, in which the aqueous phase is eliminated in a liquid state. The report does not contain polymer in the wastewater. EP-A 0 683 028 describes a method for dehydrating a two-phase fluid mixture of a thermoplastic plastic melt and an aqueous phase in a reverse two-way screw extruder. In the meantime, the gelation of the plastic latex is directly performed in the gelling zone of the capture machine under the action of shear force at a temperature in the plastic thermoplastic range. The melt is pushed partially full of the screw lead ' and at least one of the screw leads constitutes a narrow and steep pressure gradient ', loading the solidified melt with cohesion. In this way, before the realm of the solidified melt, it flows under gravity, so that the cohesive water phase does not remain in contact with the solidified melt. Using this method you can make up to 5 5 weight. /. Original 539603 V. Description of the invention (2) The water content of the milky polymer of the starting water component is reduced to only 8% by weight. In the exhaust extruder, the remaining volatile components can be continuously and continuously removed in the exhaust zone forward or backward. The granules finally obtained at the granulation nozzle had a residual moisture of only 0.06% by weight. For the three-phase milky polymer, the residual polymer content as an organic substance in the waste water to be pressed out is in the range of 0.4% by weight. DE 1 97 1 8 597 C1 describes a method for dehydrating a two-phase fluid mixture composed of a thermoplastic phase and an aqueous phase. The method uses a two-phase fluid mixture to gel in an extruder, and has a dewatering zone with a convection screw In the twin-screw extruder, the gel is dehydrated and the moisture component is removed by exhaust. A single-screw extruder or a twin-screw extruder is used as the first extruder, in which the twin-screw extrusion The machine is equipped with a synchronous screw. For three-phase fluid polymers, a residual polymer content in the range of 0.35% by weight will be obtained in the pressurized wastewater. Problems and solutions For the dehydration of a thermoplastic plastic melt and water phase into a two-phase fluid mixture, it uses the gelation of the plastic melt and removes water from the solidified melt. There are problems in the extruder device. Wastewater It often contains undesirably high amounts of polymers. This problem is especially seen in milky polymers with a small particle size, which is usually difficult to gel; this problem also exists in milky polymers with larger particle sizes. Although it can be gelled and only a small amount of polymer components are present in the wastewater under standard conditions, the throughput rate must be increased. This will usually impair gelation efficiency, so the polymer content in the wastewater will rise again. The separated water phase is contaminated because it contains polymers and cannot be reused, especially missing. The polymer content in the waste increases the load of the sedimentation tank during wastewater treatment (CSB 値). -4- 603603 5. Description of the invention (3) As a result, the loss of the polymer reduces the yield of the thermoplastic plastic melt. It is therefore necessary to find a way to reduce the polymer content in the wastewater. This problem is solved by a method of reducing the polymer content in the wastewater. The two-phase fluid mixture formed by the thermoplastic plastic melt and the water phase is caused by the gelation of the plastic melt and the melting from the solidified melt in an extruder device. It is solved by removing the water pressure by the body, which is characterized in that the two-phase fluid mixture is added to the extruder device to indirectly introduce superheated steam with a temperature of at least 280t. Implementation of the invention The method of the present invention is suitable for a two-phase fluid mixture formed from a thermoplastic plastic melt and an aqueous phase to reduce the polymer content in the dewatered wastewater. The method is used to gel the plastic melt in an extruder device. Water is removed from the solidified melt by pressure. This method is particularly suitable for milky polymers having an average particle size (weight average) of 50 to 130 nanometers, as described in DE 3 8 42 796 C2 and specific examples. The inconsistency of the particle size may be, for example, 0.2 or less. The key point here is that the emulsion polymer is composed of latex particles composed of a thermoplastic solid phase and a crosslinked tough phase that can be used as a double-layer impact toughness modifier. This method is further suitable for use with both good gelable milky polymers 'which have an average particle size of more than 130 nm to 500 nm', especially from 250 to 400 nm, if the device is to be processed with increased throughput And for this reason, the polymer content in the wastewater increased again unexpectedly. Among them, it is especially called as a three-layer impact toughness modifier and used in polymethyl methacrylate emulsion polymer, as described in EP-A 0 683 028 539603 4) Described in DE 1 97 1 8 597 C1 and specific examples. If the methods described in EP-A 0 683 028 and DE 1 97 1 8 597 C1 are used to increase the polymer passing rate, for example, doubling, it will hinder the rule of heating and impair the gelation efficiency. As a result, the originally extremely low polymer content in the wastewater increased to more than 1% by weight, or even more than 2% by weight. If combined with the present invention, the plutonium has been reduced again by less than 1% by weight, especially below 0.5% by weight, in high throughput rates. The invention is therefore particularly suitable for latexes, which can usually contain 30 to 50% by weight of dispersed plastic particles, with an average particle size of, for example, 100 to 500 nm. The total relative water phase is 70 to 50% by weight, including all dissolved emulsifiers, gelling agents or other auxiliaries and impurities that may be present. The latex particles are made of thermoplastic plastic and can be processed into a molten state in an extruder. In addition, thermoplastics fall within the glass transition temperature range of 50 to 300 ° C or a temperature range that is sufficiently resistant to decomposition. The melting temperature in a twin screw extruder is usually between 100 and 250 ° C. The important types of thermoplastics are copolymers based on butadiene, styrene, and acrylonitrile as needed, as well as polyvinyl chloride, polyacrylate, or polymethacrylate. More important types are the various latexes of heterophasic thermoplastics, which contain latex particles with a thermoplastic solidified phase and a crosslinked tough phase. In this method, if necessary, other thermoplastics which are added to the twin-screw extruder in a solid or molten state can be used, and they are mixed with or compatible with the solidified phase plastic of the latex. The solid phase plastic is preferably composed of polymethyl methacrylate, and the tough phase plastic is mostly composed of cross-linked polybutyl acrylate. If it is to adjust the refractive index -6- 539603 V. Description of the invention (5) to match Polymethyl methacrylate can be mixed with styrene or benzyl acrylate for polymerization. A typical blend of this type, for example, contains 4 to 50% by weight of a heterophasic latex-plastic which may consist of 2 to 80% by weight of a polybutyl acrylate component and 20 to 98% by weight of a polymethyl methacrylate component. Composition; and 2 to 60% by weight of thermoplastic polymethyl methacrylate plastic. If the person to be added is not in the molten state, it may also be a heterophasic plastic latex mixed with a polymethacrylate latex, and the latex polymer is processed according to the method of the present invention. Extruder devices for dehydrating emulsion polymers generally contain a gelling zone in which the latex is gelled, with an operating pressure higher than the water vapor pressure in between, which uses shear elements such as kneading-, Mixing or plugging, etc., starts the phase separation. There is another dehydration section, from which water is removed. At this time, water-soluble components such as emulsifiers or electrolytes are also separated and removed. An exhaust section is isolated from the dewatering section by a pressurized and compacted congestion section. It is also used for further dehydration. Finally, a pump section is used to re-establish pressure and handle the discharge of the grain. These functions can be distributed across multiple units or extruders. The extrusion device can be composed of a twin-screw extruder with a counter-screw, in which the gelling of the plastic melt and the removal of water from the solidified melt are carried out. Such a device and a corresponding method are contained, for example, in EP-A 0 683 028. The extrusion device can be gelled by a single-screw extruder or a twin-screw extruder with a co-rotating screw; then a twin-screw extruder with a reverse screw is used for gelation and Pressure removal and other effects. Such a device and a corresponding method are described in DE 197 18 597 C1. According to the method of the present invention, after the thermoplastic plastic melt and water phase are in place, 539603 V. Description of the invention (6) After the two-phase fluid mixture is added to the extruder, the superheated steam is directly introduced, and the temperature is The temperature is preferably 290 to 300 ° C, and particularly preferably 300 to 3 20 ° C. The corresponding pressure when introduced into the extruder is 25 to 35 bar, especially 28 to 32 bar. The amount of water vapor to be introduced may be, for example, 1 to 10 kg of water per hour, preferably 2 to 8 kg, and 4 to 6 kg, relative to the processing amount of 10 to 20 kg of the plastic / water mixture to be dehydrated. Feeding is done using suitable equipment, such as a feed pump with a material flow meter and an electric steam generator for separation. The laboratory apparatus may be provided, for example, with a steam generator having a thermal power from 10 to 15 watts. In the meantime, at the steam generator outlet, for example, hot water steam at 310 ° C, the steam pressure is in the range of about 50 bar, and at the entrance of the extruder is about 30 bar. The dehydrated plastic discharged from the twin screw extruder is in the shape of a melt. This can be achieved by the existence of granulated jets, from which many thin strips are extruded, cooled below the softening temperature, and cut into commercially-used molded pellets. However, it can also be directly extruded using a suitable extrusion die in a known manner. Plastic profiles, such as a film. EXAMPLES Example U Comparative Example) After processing, a two-stage emulsion polymer (impact toughness modifier for PMMA molding compounds) has the following composition: (inside the brackets, a single symbol is used to indicate a shortened symbol) Mass ratio of body composition) Phase I: The ratio of butyl acrylate / propyl methacrylate is 98: 2 Phase Ⅱ: methyl methacrylate / butyl acrylate / 3- (2-benzotriazolyl)- Proportion of 2-hydroxy-5-third octyl benzylmethacrylate: (89.1: 8.0: 2.9) 539603 V. Description of the invention (7) I / Π mass ratio = 33.4 / 66.6 polymer phase / water Phase mass ratio = 40/60 Average particle size: about 60nm Pump a latex into a cylinder (section 1) of a sealed reverse twin screw extruder using a film metering pump with a flow rate of 15 kg / hour . The screw diameter is 34 mm. The screw is a three spiral with a pitch of 30 mm. The number of screw revolutions was 1 1 5 rpm. The gelling section is 600 mm in length and is divided into five sections starting from section 1 (sections 1 to 5). The specified temperature of each gelation zone in the extruder is: zone 1: 260 ° C / zone 2: 270 ° C / zone 3: 25 0 ° C / zone 4: 24 0 ° C / zone Segment 5: 170 ° C. A dewatering section follows section 5 and is equipped with a non-return screw with a length of 120 mm. In the dewatering section, a gap of 2 mm wide and 60 mm long is opened at the lowest point of the two cylinders. Under these two openings, the device collecting groove is pressed. The collection tank for the precipitated water is maintained at a nitrogen pressure of 40 bar via a line. The valve was used to control the liquid level to discharge 5.27 kg / h of water. The injection of the exhaust extruder to the rear is adjusted through a valve to keep the melt pressure in front of the valve constant at 80 bar. The injection in the exhaust extruder maintains 8% by weight of water. In the exhaust extruder (screw diameter 30 mm), the volatile part of the residue is eliminated through two exhaust sections. The first exhaust pressure was 100 mbar, and the subsequent exhaust pressure was 10 mbar. Extrudate or pellets obtained in the pelletizing die nozzle -9-539603 V. Description of the invention (8) It has a residual moisture of 0.06% by weight. The water precipitated in the dewatering section has a polymer content of 2% by weight. Xuanshi Example 2 (according to the present invention) The method as in Example 1, except that the milky polymer in the second stage is added to the extrusion device and directly added with superheated steam.
在區段1和區段2之間接入一管以供饋入過熱水蒸汽， 其爲經過具有物料流量計而用於蒸汽之給水泵，並由一電 熱且爲分離之蒸汽產生器所產生。在蒸汽產生器內之熱板 設定爲12仟瓦。在是處水被定量轉變爲31 0°C之熱蒸汽。 在蒸汽產生器出口處將蒸汽壓調整維持在50巴，而在擠 押機出口則調整壓力約爲30巴（隨蒸汽供給量和缸內溫度 而定）。爲了管路和進料閥之淋水，裝有一淋水循環。A pipe is connected between section 1 and section 2 for feeding superheated steam, which is passed through a feed water pump with a material flow meter for steam, and is generated by an electric and separate steam generator. The hot plate in the steam generator is set to 12 watts. Water is quantitatively transformed into hot steam at 31 0 ° C. The steam pressure is maintained at 50 bar at the steam generator outlet and about 30 bar at the extruder outlet (depending on the steam supply and the temperature in the cylinder). In order to spray water from the pipeline and the feed valve, a shower circuit is installed.
在導入5公斤/小時之熱蒸汽於1 5公斤膠液/水-混合物 時，在區段1之缸壁溫度從150升至190°C ’而在區段2 將由約220°C升至26CTC。在區段5中於脫水段前所給之 冷水量由9公斤/小時增高至1 3公斤/小時。另一種情形爲 若熔體溫度過高，而且因而使熔體黏度過低’可能導致熔 體越過水道而流失，並因而收縮堵塞。 在脫水區段中所析之水約有0.3重量°/❶之聚合物含量。 -10-When introducing 5 kg / h of hot steam to 15 kg of glue / water-mixture, the temperature of the cylinder wall in section 1 will rise from 150 to 190 ° C 'and in section 2 will rise from about 220 ° C to 26CTC . The amount of cold water given in the section 5 before the dehydration section increased from 9 kg / hour to 13 kg / hour. Another situation is that if the melt temperature is too high, and thus the melt viscosity is too low ', it may cause the melt to flow through the water channel and be lost, and thus shrink and block. The water precipitated in the dewatering section has a polymer content of about 0.3% by weight / degree. -10-